EP2033702A1 - Method for removing mercury from exhaust combustion gases - Google Patents

Method for removing mercury from exhaust combustion gases Download PDF

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Publication number
EP2033702A1
EP2033702A1 EP07115662A EP07115662A EP2033702A1 EP 2033702 A1 EP2033702 A1 EP 2033702A1 EP 07115662 A EP07115662 A EP 07115662A EP 07115662 A EP07115662 A EP 07115662A EP 2033702 A1 EP2033702 A1 EP 2033702A1
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EP
European Patent Office
Prior art keywords
solution
adsorbent
mercury
exhaust gases
combustion exhaust
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EP07115662A
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German (de)
French (fr)
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EP2033702B1 (en
Inventor
Hermann Dr. Winkler
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Steag Energy Services GmbH
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Evonik Energy Services GmbH
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Priority to DK07115662.4T priority Critical patent/DK2033702T3/en
Application filed by Evonik Energy Services GmbH filed Critical Evonik Energy Services GmbH
Priority to SI200730566T priority patent/SI2033702T1/en
Priority to ES07115662T priority patent/ES2359091T3/en
Priority to PT07115662T priority patent/PT2033702E/en
Priority to PL07115662T priority patent/PL2033702T3/en
Priority to AT07115662T priority patent/ATE495812T1/en
Priority to DE502007006314T priority patent/DE502007006314D1/en
Priority to EP07115662A priority patent/EP2033702B1/en
Priority to CA2616540A priority patent/CA2616540C/en
Priority to US12/082,761 priority patent/US7727307B2/en
Priority to TW097130913A priority patent/TWI355289B/en
Priority to ZA200807352A priority patent/ZA200807352B/en
Priority to AU2008207555A priority patent/AU2008207555B2/en
Priority to KR1020080086802A priority patent/KR101124058B1/en
Priority to JP2008225927A priority patent/JP2009061450A/en
Publication of EP2033702A1 publication Critical patent/EP2033702A1/en
Application granted granted Critical
Publication of EP2033702B1 publication Critical patent/EP2033702B1/en
Priority to JP2014109033A priority patent/JP2014155927A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • the present invention relates to a method for removing mercury from combustion exhaust gases.
  • Exhaust gases from incinerators such as power plants or waste incinerators, contain a variety of pollutants that must be removed from the combustion exhaust gases before they are released into the environment.
  • Modern incinerators are equipped with emission control systems, which i.a. Remove sulfur dioxide, nitrogen oxides, hydrogen halides and entrained ash contained in combustion exhaust gases.
  • the combustion exhaust gases contain traces of heavy metals, which must be removed from the combustion exhaust gases because of their toxicity.
  • a particularly toxic heavy metal contained in the combustion exhaust gases is mercury. This is washed in conventional flue gas desulphurization (REA) from the combustion exhaust gases and enters with the waste water of the flue gas desulfurization in the sewage system.
  • REA flue gas desulphurization
  • the mercury dissolved in the waste water is precipitated in sparingly soluble form together with other solids than RAA sludge.
  • this RAA sludge can not be incinerated, but must be disposed of as hazardous waste.
  • a method for purifying combustion exhaust gases is known, with which mercury can be removed from combustion exhaust gases.
  • the combustion exhaust gases are subjected to a wet scrubbing, wherein this wet scrubbing is carried out with the addition of activated carbon particles which adsorb heavy metals, and in particular mercury.
  • the activated carbon particles are separated from the resulting wet scrubbing suspension and recirculated into the wet scrubbing, with a portion of the particles branched off is and is desorbed thermally.
  • the thermal desorption is technically complex and therefore expensive.
  • the invention is therefore based on the object to provide a simple and inexpensive method for removing mercury from combustion exhaust gases.
  • the object is achieved by a method in which first mercury contained in the combustion exhaust gases is brought into contact with an adsorbent, wherein the mercury is largely adsorbed by the adsorbent.
  • first mercury contained in the combustion exhaust gases is brought into contact with an adsorbent, wherein the mercury is largely adsorbed by the adsorbent.
  • adsorbent for the purposes of this application, the use of the term "mercury" includes mercury in oxidation states 0, 1 and 2.
  • the adsorbent can be blown into the combustion exhaust gases, for example in the form of fine particles.
  • the mercury from the adsorbent is largely adsorbed directly from the combustion exhaust gases.
  • the adsorbent may further be added in a wet working step, such as desulfurization.
  • the mercury contained in the combustion exhaust gases is initially partly in solution and is largely adsorbed by this of the adsorbent. It is also possible to combine adsorption from the gas phase and from liquid by introducing the adsorbent into the combustion exhaust gases upstream of a wet working step.
  • adsorbents which can be used are the customary adsorbents, for example bentonite, silica gel and activated carbon.
  • the adsorbent is separated from the combustion exhaust gases after adsorption. Such a separation can be carried out with all devices known to the person skilled in the art.
  • the mercury-laden adsorbent is separated from the combustion exhaust gases, it is contacted with an aqueous solution containing an oxidizer.
  • the present process is not limited to any particular oxidizing agent.
  • hypochlorite chlorine dioxide or chlorine gas can be used.
  • Particularly preferred is the use of hypochlorite, as this, compared to gaseous oxidants, is easy to handle and is available at low cost in larger quantities. It has also been found that when using hypochlorite only a short residence time of the adsorbent in the aqueous solution is necessary to dissolve the mercury from the adsorbent.
  • the Hg 2+ -containing solution is separated from the adsorbent and any other additional solids present.
  • the mercury content of the adsorbent and any other existing solids is now so low that they can be burned, for example.
  • the mercury is removed from the solution.
  • the removal of the mercury from the solution can be carried out by any method known to those skilled in the art.
  • the inventive method has several advantages over known methods.
  • the wastewater produced during the treatment of the combustion gases for example from a REA scrubber, is only very small Measured contaminated with mercury, since the addition of the adsorbent, the mercury passes to this.
  • the mercury can be separated from the adsorbent in a systemically simple and thus cost-effective manner with a solution comprising an oxidizing agent and can be removed from the solution after this separation using a known method.
  • the Hg 2+ can be removed from the solution in a particularly cost-effective and uncomplicated manner by adding a precipitant to the Hg 2+ -containing solution which forms a sparingly soluble precipitate with Hg 2+ , and separates it from the solution.
  • a precipitant sulfides, and in particular organosulfides are preferred.
  • the mercury sulphide which forms in the reaction with the precipitant is stable over a wide pH range and can be further processed as a pigment. It is also advantageous that mercury sulphide is practically insoluble in water and thus is classified as non-toxic.
  • organosulfides are particularly preferred, as they form with the mercury "larger" organo-mercury sulfide molecules as compared to pure mercury sulfide, which precipitate more readily from the corresponding solution.
  • the Hg 2+ can be removed from the solution by contacting the solution with an ion exchanger.
  • This type of removal of mercury from the solution is also easy to implement in terms of plant technology.
  • ion exchange resins various IMAC TM variants or 1,3,5-triazine-2,4,6-trithiol can be used.
  • the inventive method is not limited to these resins.
  • Particularly preferred are ion exchange resins with functional HS groups, since with these a particularly efficient removal of the mercury from the solution is possible.
  • Hg 0 contained in the combustion exhaust gases is oxidized, prior to the bringing into contact of mercury contained in the combustion exhaust gases with the adsorbent. Since the adsorbents preferentially adsorb Hg 2+ , by oxidizing Hg 0 contained in the combustion exhaust gases, the Hg concentration in the purified combustion exhaust gas can be further lowered. However, such oxidation is only necessary and useful if the Hg 0 content of the combustion gases is too high.
  • the oxidation of Hg 0 can be carried out, for example, by catalysts or halogens, but other process steps known to those skilled in the art for the oxidation of Hg 0 are also conceivable.
  • REA scrubbers When cleaning the combustion gases, these are desulfurized, among other things.
  • This desulfurization takes place in so-called REA scrubbers, in which the sulfur dioxide contained in the combustion exhaust gases is converted to a sulfate in the presence of an oxidizing agent.
  • the sulfate is separated and - depending on the desulfurization - processed or landfilled.
  • This separation step can also be used to separate the adsorbent from other solids by feeding the adsorbent to the combustion exhaust gases before or in the REA scrubber. In this way, the separation of the sulfate can be combined with the separation of the adsorbent, which reduces the plant-technical overhead and thus the cost.
  • This separation can be realized particularly simply by separating the solids formed in the REA scrubber by centrifugal separation from the adsorbent. Such a separation creates two phases. On the one hand, the heavy crystalline calcium sulfate, and on the other a waste water suspension, which contains, among other things, the adsorbent and other solids, in particular metal hydroxides. After the gypsum has been separated, the adsorbent, along with the other solids, is separated from the effluent.
  • activated carbon Since activated carbon has a particularly large active surface area and therefore only has to be added to the combustion exhaust gases in very small amounts, activated carbon is preferably used as the adsorbent.
  • the use of activated carbon also has the advantage that it can be easily separated in the subsequent step. Further, the activated carbon may easily be burned after contacting with an oxidant-containing solution with other solids to be separated.
  • peat-derived activated carbon as it has a larger internal surface compared to other types of activated carbon.
  • the adsorbent is separated and recirculated after being contacted with a solution containing an oxidizer. In this way, the initial cost of the adsorbent can be reduced and the environmental pollution resulting from combustion of the adsorbent can be avoided.
  • the embodiment of the inventive method shown in the flowchart relates to a combustion exhaust gas purification for a 500 MW block of a power plant.
  • the combustion exhaust gases reach the denitrification device (2), with which the nitrogen oxides are removed from the combustion exhaust gases.
  • the denitrification device can be operated in accordance with a method known to those skilled in the art, such as selective non-catalytic or catalytic denitrification.
  • the denitrated exhaust gases pass into a dedusting system (3), in which flue dust is removed from the combustion exhaust gases becomes.
  • a dedusting system (3) in which flue dust is removed from the combustion exhaust gases becomes.
  • an electrostatic precipitator is usually used to dedust the combustion gases.
  • the sulfur dioxide present in the combustion exhaust gases is removed by a spray adsorption process in which a basic hydrated lime suspension is sprayed into the combustion exhaust gases to be purified.
  • the resulting in the reaction with sulfur dioxide CaSO 3 is oxidized, for example, with atmospheric oxygen to CaSO 4 .
  • Hg 1+ which may still be present in the combustion exhaust gases, is also oxidized to Hg 2+ .
  • other desulfurization processes may be used - for example desulfurization with ammonia.
  • activated carbon particles are added as adsorbent.
  • the activated carbon particles adsorb the Hg 2+ transferred from the combustion exhaust gases to the REA scrubber solution.
  • part of the mercury present in the combustion exhaust gases is already adsorbed by the activated carbon particles from the combustion exhaust gases themselves.
  • the unadsorbed mercury goes into solution in the REA scrubber where it is adsorbed by the activated carbon particles.
  • the resulting in the REA scrubber suspension containing, inter alia, gypsum, other solids and activated carbon particles is fed into a gypsum cyclone (5), which separates the resulting in the REA scrubber suspension into two phases, namely in the heavy crystalline CaSO 4 and a suspension containing the light activated carbon particles as well as other amorphous and thus light solids such as dust and metal hydroxides.
  • the degree of gypsum whiteness is only marginally reduced by the addition of activated carbon, from about 74% to 72%.
  • the gypsum cyclone (5) leaving suspension is fed into a wastewater cyclone (6).
  • this wastewater cyclone (6) a part of the waste water is separated from the suspension and gives a suspension with a higher solids content.
  • the volume of this suspension from the wastewater cyclone (6) is greatly reduced, so that subsequent process steps can be made less expensive plant technology.
  • the wastewater cyclone (6) leaving wastewater has a mercury concentration of only about 10 micrograms / l.
  • the wastewater is partially recirculated to the process, or it is fed to a wastewater treatment plant. Due to the low mercury content, the RAA sludge produced in the wastewater plant can be incinerated - landfilling is no longer required.
  • the inventive method is not limited to the illustrated in this embodiment separation of the activated carbon and other solids from the wastewater or the combustion gases.
  • the separation can also be carried out with other separation methods known to the person skilled in the art.
  • the above separation method is preferred because it allows separation into gypsum, waste water and a solids-containing suspension with simple means.
  • an aqueous sodium hypochlorite solution is introduced into the suspension from the wastewater cyclone (6), which contains the activated carbon particles and further solids initiated with a pH of about 6.5.
  • a suitable stirring device per liter of suspension, 1 - 4 ml of an approx. 13% sodium hypochlorite solution are introduced.
  • the solution is mixed with a suitable stirring device.
  • oxidants in a different pH range.
  • the mercury dissolves again from the activated carbon and goes into solution as Hg 2+ .
  • the solution is treated with a flocculant and / or a flocculant and with Ca (to increase the pH of the solution).
  • OH) 2 offset The solution is adjusted to a pH of about 8.5.
  • the increase in the pH occurs on the one hand due to legal requirements, which state that wastewater from a wastewater treatment plant must have a lying in a certain pH window pH value, and on the other, to provide a gypsum desaturation of the solution.
  • This means that upon addition of the Ca (OH) 2 additional calcium sulfate precipitates out of the solution.
  • further metal hydroxides such as, for example, nickel hydroxide and copper hydroxide, precipitate out of the solution.
  • Flocculants are substances which influence particles in a suspension in such a way that they aggregate into flakes (microflakes) and can therefore be removed from the suspension.
  • the flocculant used in the present embodiment is preferably iron (III) chloride, iron (III) sulfate or a mixture of these salts. Which of these salts is used depends on the current availability. Addition of these salts produces a voluminous Fe (OH) 3 precipitate which coalesces with other less bulky solids.
  • a so-called flocculation aid may be used be added, which causes the aggregation of solid particles into larger units (macroflakes), which can settle faster due to their larger mass and can be separated easily.
  • anionic polymers are preferably added in the present embodiment. Whether and to what extent a flocculant or a flocculant is added depends on the composition of the suspension and thus on the process control and the composition of the combustion exhaust gases.
  • the solids present in the suspension after the above treatment, which are now substantially free of mercury, are subsequently separated from the mercury-containing solution in a filter press.
  • the solids accumulate per day about 20 tons of solids at which the mercury content is below 10g / t. Due to this low mercury content, the solids can be incinerated and thus there are no costs for landfilling.
  • the solids may also be separated by sedimentation or flotation.
  • the mercury-containing solution is treated with an organosulfide, a flocculant and a flocculant.
  • an organosulfide As a flocculant iron (III) chloride is preferably used, since this is inexpensive to obtain.
  • an oxidation-resistant organosulfide is preferably added because the solution may have a high oxidation potential. To avoid settling of the Organoquecksilbersulfids already at this time, the solution is mixed at this stage with a suitable stirring device.
  • the solids are separated and deposited via a membrane filter press.
  • a membrane filter press In the exemplary embodiment described here, about 0.2 t of organo-mercury sulfide-containing waste accumulates per day.

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Abstract

The mercury present in the flue gas is brought in contact with activated carbon. The mercury is adsorbed in the activated carbon. The adsorbed mercury is separated from the carbon. The carbon is brought in contact with an oxidizing reagent such as hypochlorite, chlorine dioxide or chlorine gas. The adsorbed mercury is desorbed and dissolves in the form of Hg 2> +>in a solution. The Hg 2> +>enriched solution is separated from the carbon. The Hg 2> +>is removed from the solution by mixing with an organosulfide precipitating reagent or bringing the solution to contact with an ion exchanger.

Description

Die vorliegende Erfindung betrifft ein Verfahren zum Entfernen von Quecksilber aus Verbrennungsabgasen.The present invention relates to a method for removing mercury from combustion exhaust gases.

Abgase aus Verbrennungsanlagen, wie beispielsweise Kraftwerke oder Müllverbrennungsanlagen, enthalten eine Vielzahl von Schadstoffen, die aus den Verbrennungsabgasen entfernt werden müssen, bevor diese an die Umwelt abgegeben werden. Moderne Verbrennungsanlagen sind mit Abgasreinigungsanlagen ausgerüstet, die u.a. in den Verbrennungsabgasen enthaltenes Schwefeldioxid, Stickoxide, Halogenwasserstoffe und mitgeführte Asche entfernen.Exhaust gases from incinerators, such as power plants or waste incinerators, contain a variety of pollutants that must be removed from the combustion exhaust gases before they are released into the environment. Modern incinerators are equipped with emission control systems, which i.a. Remove sulfur dioxide, nitrogen oxides, hydrogen halides and entrained ash contained in combustion exhaust gases.

Neben den oben genannten Schadstoffen enthalten die Verbrennungsabgase Spuren von Schwermetallen, die aufgrund ihrer Toxizität aus den Verbrennungsabgasen entfernt werden müssen. Ein besonders giftiges, in den Verbrennungsabgasen enthaltenes Schwermetall ist Quecksilber. Dieses wird bei üblichen Rauchgas-Entschwefelungsanlagen (REA) aus den Verbrennungsabgasen gewaschen und gelangt mit dem Abwasser der Rauchgas-Entschwefelungsanlagen in die Abwasseranlage. In der Abwasseranlage wird das in dem Abwasser gelöste Quecksilber in schwerlöslicher Form zusammen mit anderen Feststoffen als RAA-Schlamm ausgefällt. Aufgrund der Kontaminierung mit Quecksilber kann dieser RAA-Schlamm jedoch nicht verbrannt werden, sondern muss als Sondermüll entsorgt werden.In addition to the above-mentioned pollutants, the combustion exhaust gases contain traces of heavy metals, which must be removed from the combustion exhaust gases because of their toxicity. A particularly toxic heavy metal contained in the combustion exhaust gases is mercury. This is washed in conventional flue gas desulphurization (REA) from the combustion exhaust gases and enters with the waste water of the flue gas desulfurization in the sewage system. In the sewage plant, the mercury dissolved in the waste water is precipitated in sparingly soluble form together with other solids than RAA sludge. However, due to contamination with mercury, this RAA sludge can not be incinerated, but must be disposed of as hazardous waste.

Aus der EP 0 792 186 B1 ist ein Verfahren zum Reinigen von Verbrennungsabgasen bekannt, mit dem Quecksilber aus Verbrennungsabgasen entfernt werden kann. Dazu werden die Verbrennungsabgase einer Nasswäsche unterzogen, wobei diese Nasswäsche unter Zugabe von Aktivkohlepartikeln durchgeführt wird, die Schwermetalle, und insbesondere Quecksilber, adsorbieren. Anschließend werden die Aktivkohlepartikel aus der bei der Nasswäsche entstehenden Suspension abgetrennt und in die Nasswäsche rezirkuliert, wobei ein Teil der Partikel abgezweigt wird und thermisch desorbiert wird. Die thermische Desorption ist anlagentechnisch aufwendig und damit kostenintensiv.From the EP 0 792 186 B1 A method for purifying combustion exhaust gases is known, with which mercury can be removed from combustion exhaust gases. For this purpose, the combustion exhaust gases are subjected to a wet scrubbing, wherein this wet scrubbing is carried out with the addition of activated carbon particles which adsorb heavy metals, and in particular mercury. Subsequently, the activated carbon particles are separated from the resulting wet scrubbing suspension and recirculated into the wet scrubbing, with a portion of the particles branched off is and is desorbed thermally. The thermal desorption is technically complex and therefore expensive.

Der Erfindung liegt daher die Aufgabe zugrunde, ein einfaches und kostengünstiges Verfahren zum Entfernen von Quecksilber aus Verbrennungsabgasen bereitzustellen.The invention is therefore based on the object to provide a simple and inexpensive method for removing mercury from combustion exhaust gases.

Die Aufgabe wird gelöst durch ein Verfahren, bei dem zunächst in den Verbrennungsabgasen enthaltenes Quecksilber mit einem Adsorptionsmittel in Kontakt gebracht wird, wobei das Quecksilber von dem Adsorptionsmittel weitgehend adsorbiert wird. Im Rahmen dieser Anmeldung umfasst die Verwendung des Begriffs "Quecksilber" Quecksilber in den Oxidationsstufen 0, 1 und 2.The object is achieved by a method in which first mercury contained in the combustion exhaust gases is brought into contact with an adsorbent, wherein the mercury is largely adsorbed by the adsorbent. For the purposes of this application, the use of the term "mercury" includes mercury in oxidation states 0, 1 and 2.

Bei dem erfindungsgemäßen Verfahren kann das Adsorptionsmittel beispielsweise in Form von feinen Partikeln in die Verbrennungsabgase geblasen werden. In einem solchen Fall wird das Quecksilber von dem Adsorptionsmittel weitgehend direkt aus den Verbrennungsabgasen adsorbiert. Das Adsorptionsmittel kann ferner bei einem Nassarbeitsschritt, wie beispielsweise dem Entschwefeln, zugefügt werden. In diesem Fall geht das in den Verbrennungsabgasen enthaltene Quecksilber zunächst zum Teil in Lösung und wird aus dieser von dem Adsorptionsmittel weitgehend adsorbiert. Es ist auch möglich, die Adsorption aus der Gasphase und aus Flüssigkeit zu kombinieren, indem das Adsorptionsmittel stromauf eines Nassarbeitsschritts in die Verbrennungsabgase eingeleitet wird.In the method according to the invention, the adsorbent can be blown into the combustion exhaust gases, for example in the form of fine particles. In such a case, the mercury from the adsorbent is largely adsorbed directly from the combustion exhaust gases. The adsorbent may further be added in a wet working step, such as desulfurization. In this case, the mercury contained in the combustion exhaust gases is initially partly in solution and is largely adsorbed by this of the adsorbent. It is also possible to combine adsorption from the gas phase and from liquid by introducing the adsorbent into the combustion exhaust gases upstream of a wet working step.

Als Adsorptionsmittel können die gängigen Adsorptionsmittel, wie beispielsweise Bentonit, Kieselgel und Aktivkohle, verwendet werden.The adsorbents which can be used are the customary adsorbents, for example bentonite, silica gel and activated carbon.

Das Adsorptionsmittel wird nach der Adsorption von den Verbrennungsabgasen getrennt. Eine derartige Trennung kann mit allen dem Fachmann bekannten Vorrichtungen durchgeführt werden.The adsorbent is separated from the combustion exhaust gases after adsorption. Such a separation can be carried out with all devices known to the person skilled in the art.

Nachdem das mit Quecksilber beladene Adsorptionsmittel von den Verbrennungsabgasen getrennt wurde, wird es mit einer ein Oxidationsmittel enthaltenden wässrigen Lösung in Kontakt gebracht.After the mercury-laden adsorbent is separated from the combustion exhaust gases, it is contacted with an aqueous solution containing an oxidizer.

Es hat sich nun überraschenderweise gezeigt, dass mit einer solchen Behandlung des Adsorptionsmittels das Quecksilber fast quantitativ wieder von diesem entfernt werden kann und als Hg2+ in die wässrige Lösung übergeht. Eine Erwärmung der wässrigen Lösung ist dabei nicht notwendig, wodurch dieser Arbeitsschritt sehr kostengünstig realisiert werden kann.It has now surprisingly been found that with such a treatment of the adsorbent, the mercury can be almost quantitatively removed again from this and passes as Hg 2+ in the aqueous solution. A heating of the aqueous solution is not necessary, whereby this step can be realized very inexpensively.

Das vorliegende Verfahren ist dabei auf kein bestimmtes Oxidationsmittel beschränkt. Beispielsweise können Hypochlorit, Chlordioxid oder Chlorgas verwendet werden. Es ist auch möglich, das Quecksilber durch katalytische Oxidation mit Luft, ggf. in der Gegenwart von einem Cu2+-Salz, von dem Adsorptionsmittel zu lösen. Besonders bevorzugt ist die Verwendung von Hypochlorit, da dieses, im Vergleich zu gasförmigen Oxidationsmitteln, einfach zu handhaben ist und in größeren Mengen preisgünstig verfügbar ist. Es hat sich ferner gezeigt, dass bei Verwendung von Hypochlorit nur eine kurze Verweilzeit des Adsorptionsmittels in der wässrigen Lösung notwendig ist, um das Quecksilber von dem Adsorptionsmittel zu lösen.The present process is not limited to any particular oxidizing agent. For example, hypochlorite, chlorine dioxide or chlorine gas can be used. It is also possible to dissolve the mercury by catalytic oxidation with air, optionally in the presence of a Cu 2+ salt, from the adsorbent. Particularly preferred is the use of hypochlorite, as this, compared to gaseous oxidants, is easy to handle and is available at low cost in larger quantities. It has also been found that when using hypochlorite only a short residence time of the adsorbent in the aqueous solution is necessary to dissolve the mercury from the adsorbent.

Da bestimmte Oxidationsmittel nur in bestimmten pH-Bereichen arbeiten, kann man durch entsprechende Wahl des Oxidationsmittels bereits bei diesem Schritt des Verfahrens einen pH-Bereich einstellen, der für nachfolgende Arbeitsschritte am günstigsten ist.Since certain oxidizing agents work only in certain pH ranges, it is possible to set a pH range, which is the most favorable for subsequent working steps, by appropriate choice of the oxidizing agent already in this step of the method.

Nachdem das Quecksilber von dem Adsorptionsmittel gelöst wurde, wird die Hg2+-haltige Lösung von dem Adsorptionsmittel und ggf. vorhandenen weiteren Feststoffen getrennt. Der Quecksilbergehalt des Adsorptionsmittels sowie ggf. vorhandener weiterer Feststoffe ist nun so gering, dass diese beispielsweise verbrannt werden können.After the mercury has been released from the adsorbent, the Hg 2+ -containing solution is separated from the adsorbent and any other additional solids present. The mercury content of the adsorbent and any other existing solids is now so low that they can be burned, for example.

Nach Abtrennung des Adsorptionsmittels wird das Quecksilber aus der Lösung entfernt. Die Entfernung des Quecksilbers aus der Lösung kann mit jedem dem Fachmann bekannten Verfahren durchgeführt werden.After separation of the adsorbent, the mercury is removed from the solution. The removal of the mercury from the solution can be carried out by any method known to those skilled in the art.

Das erfindungsgemäße Verfahren weist mehrere Vorteile gegenüber bekannten Verfahren auf. Zum einen ist das bei der Behandlung der Verbrennungsabgase entstehende Abwasser, beispielsweise aus einem REA-Wäscher, nur noch in sehr geringem Maße mit Quecksilber verunreinigt, da durch die Zugabe des Adsorptionsmittels das Quecksilber auf dieses übergeht. Dies bedingt, das in einer nachgeschalteten Abwasseranlage anfallender RAA-Schlamm nicht mit Quecksilber kontaminiert ist, und dieser daher nicht als Sondermüll entsorgt werden muss, sondern verbrannt werden kann. Ferner kann das Quecksilber auf eine anlagentechnisch einfache und somit kostengünstige Art und Weise wieder mit einer ein Oxidationsmittel aufweisenden Lösung von dem Adsorptionsmittel getrennt werden und kann nach dieser Trennung mit einem bekannten Verfahren aus der Lösung entfernt werden.The inventive method has several advantages over known methods. On the one hand, the wastewater produced during the treatment of the combustion gases, for example from a REA scrubber, is only very small Measured contaminated with mercury, since the addition of the adsorbent, the mercury passes to this. This requires that in a downstream sewage plant resulting RAA sludge is not contaminated with mercury, and therefore does not have to be disposed of as hazardous waste, but can be burned. Furthermore, the mercury can be separated from the adsorbent in a systemically simple and thus cost-effective manner with a solution comprising an oxidizing agent and can be removed from the solution after this separation using a known method.

Besonders kostengünstig und anlagentechnisch unkompliziert kann das Hg2+ aus der Lösung entfernt werden, indem die Hg2+-haltige Lösung mit einem Fällungsmittel versetzt wird, das mit Hg2+ einen schwerlöslichen Niederschlag bildet, und dieser von der Lösung abgetrennt wird. Als Fällungsmittel sind Sulfide, und insbesondere Organosulfide bevorzugt. Das sich bei der Umsetzung mit dem Fällungsmittel bildende Quecksilbersulfid ist über einen weiten pH-Bereich beständig und kann als Pigment weiterverarbeitet werden. Vorteilhaft ist ferner, dass Quecksilbersulfid in Wasser praktisch unlöslich ist und damit als ungiftig einzustufen ist. Die Verwendung von Organosulfiden ist besonders bevorzugt, da diese mit dem Quecksilber im Vergleich zu reinem Quecksilbersulfid "größere" Organoquecksilbersulfid-Moleküle bilden, die leichter aus der entsprechende Lösung ausfallen. Je geringer der Quecksilbergehalt der Rauchgase ist, desto eher empfiehlt sich die Verwendung von Organosulfiden, um so einen möglichst geringen Quecksilbergehalt des gereinigten Abwassers zu ermöglichen.The Hg 2+ can be removed from the solution in a particularly cost-effective and uncomplicated manner by adding a precipitant to the Hg 2+ -containing solution which forms a sparingly soluble precipitate with Hg 2+ , and separates it from the solution. As precipitants, sulfides, and in particular organosulfides are preferred. The mercury sulphide which forms in the reaction with the precipitant is stable over a wide pH range and can be further processed as a pigment. It is also advantageous that mercury sulphide is practically insoluble in water and thus is classified as non-toxic. The use of organosulfides is particularly preferred, as they form with the mercury "larger" organo-mercury sulfide molecules as compared to pure mercury sulfide, which precipitate more readily from the corresponding solution. The lower the mercury content of the flue gases, the sooner the use of organosulfides is recommended, in order to allow the lowest possible mercury content of the purified wastewater.

Alternativ kann das Hg2+ aus der Lösung entfernt werden, indem die Lösung mit einem Ionenaustauscher in Kontakt gebracht wird. Auch diese Art der Entfernung des Quecksilbers aus der Lösung ist anlagentechnisch einfach zu realisieren. Als Ionentauscherharze können verschiedene IMAC™-Varianten oder 1,3,5-Triazin-2,4,6-trithiol verwenden. Das erfindungsgemäße Verfahren ist jedoch nicht auf diese Harze beschränkt. Besonders bevorzugt sind Ionenaustauscherharze mit funktionellen H-S-Gruppen, da mit diesen eine besonders effiziente Entfernung des Quecksilbers aus der Lösung möglich ist.Alternatively, the Hg 2+ can be removed from the solution by contacting the solution with an ion exchanger. This type of removal of mercury from the solution is also easy to implement in terms of plant technology. As ion exchange resins, various IMAC ™ variants or 1,3,5-triazine-2,4,6-trithiol can be used. The inventive method is not limited to these resins. Particularly preferred are ion exchange resins with functional HS groups, since with these a particularly efficient removal of the mercury from the solution is possible.

In bevorzugter Weiterbildung der Erfindung wird in den Verbrennungsabgasen enthaltenes Hg0 oxidiert, und zwar vor dem in Kontakt bringen von in den Verbrennungsabgasen enthaltenem Quecksilber mit dem Adsorptionsmittel. Da die Adsorptionsmittel bevorzugt Hg2+ adsorbieren, kann durch eine Oxidation von in den Verbrennungsabgasen enthaltenem Hg0 die Hg-Konzentration in dem gereinigten Verbrennungsabgasen weiter gesenkt werden. Eine solche Oxidation ist jedoch nur dann notwendig und sinnvoll, wenn der Hg0-Gehalt der Verbrennungsabgase zu hoch ist. Die Oxidation des Hg0 kann beispielsweise durch Katalysatoren oder Halogene erfolgen, jedoch sind auch andere dem Fachmann bekannte Verfahrensschritte zur Oxidation des Hg0 vorstellbar.In a preferred embodiment of the invention, Hg 0 contained in the combustion exhaust gases is oxidized, prior to the bringing into contact of mercury contained in the combustion exhaust gases with the adsorbent. Since the adsorbents preferentially adsorb Hg 2+ , by oxidizing Hg 0 contained in the combustion exhaust gases, the Hg concentration in the purified combustion exhaust gas can be further lowered. However, such oxidation is only necessary and useful if the Hg 0 content of the combustion gases is too high. The oxidation of Hg 0 can be carried out, for example, by catalysts or halogens, but other process steps known to those skilled in the art for the oxidation of Hg 0 are also conceivable.

Bei dem Reinigen der Verbrennungsabgase werden diese u.a. entschwefelt. Diese Entschwefelung findet in sogenannten REA-Wäschern statt, in welchen das in den Verbrennungsabgasen enthaltene Schwefeldioxid in Gegenwart eines Oxidationsmittels zu einem Sulfat umgesetzt wird. Das Sulfat wird abgetrennt und - je nach Entschwefelungsverfahren - weiterverarbeitet oder deponiert. Diesen Abtrennungsschritt kann man auch zur Abtrennung des Adsorptionsmittels von anderen Feststoffen nutzen, indem das Adsorptionsmittel vor oder in dem REA-Wäscher den Verbrennungsabgasen zugeführt wird. Auf diese Weise kann die Abtrennung des Sulfats mit der Abtrennung des Adsorptionsmittels kombiniert werden, was den anlagentechnischen Mehraufwand und damit die Kosten senkt. Besonders einfach lässt sich diese Abtrennung realisieren, indem die in dem REA-Wäscher entstehenden Feststoffe durch Fliehkraftabscheidung von dem Adsorptionsmittel getrennt werden. Bei einer solchen Trennung entstehen zwei Phasen. Zum einen das schwere kristalline Calciumsulfat, und zum anderen eine Abwassersuspension, die unter anderem das Adsorptionsmittel und weitere Feststoffe, insbesondere Metallhydroxide, enthält. Nachdem der Gips abgetrennt wurde, wird das Adsorptionsmittel, zusammen mit den anderen Feststoffen, von dem Abwasser getrennt.When cleaning the combustion gases, these are desulfurized, among other things. This desulfurization takes place in so-called REA scrubbers, in which the sulfur dioxide contained in the combustion exhaust gases is converted to a sulfate in the presence of an oxidizing agent. The sulfate is separated and - depending on the desulfurization - processed or landfilled. This separation step can also be used to separate the adsorbent from other solids by feeding the adsorbent to the combustion exhaust gases before or in the REA scrubber. In this way, the separation of the sulfate can be combined with the separation of the adsorbent, which reduces the plant-technical overhead and thus the cost. This separation can be realized particularly simply by separating the solids formed in the REA scrubber by centrifugal separation from the adsorbent. Such a separation creates two phases. On the one hand, the heavy crystalline calcium sulfate, and on the other a waste water suspension, which contains, among other things, the adsorbent and other solids, in particular metal hydroxides. After the gypsum has been separated, the adsorbent, along with the other solids, is separated from the effluent.

Da Aktivkohle eine besonders große aktive Oberfläche aufweist und daher nur in sehr geringen Mengen den Verbrennungsabgasen zugesetzt werden muss, wird als Adsorptionsmittel vorzugsweise Aktivkohle verwendet. Die Verwendung von Aktivkohle hat ferner den Vorteil, dass diese bei dem nachfolgenden Arbeitsschritt einfach abgetrennt werden kann. Ferner kann die Aktivkohle nach dem in Kontakt bringen mit einer ein Oxidationsmittel enthaltenden Lösung mit anderen abzutrennenden Feststoffen problemlos verbrannt werden kann.Since activated carbon has a particularly large active surface area and therefore only has to be added to the combustion exhaust gases in very small amounts, activated carbon is preferably used as the adsorbent. The use of activated carbon also has the advantage that it can be easily separated in the subsequent step. Further, the activated carbon may easily be burned after contacting with an oxidant-containing solution with other solids to be separated.

Besonders vorteilhaft ist die Verwendung von aus Torf gewonnener Aktivkohle, da diese, verglichen mit anderen Arten von Aktivkohle, über eine größere innere Oberfläche verfügt.Particularly advantageous is the use of peat-derived activated carbon as it has a larger internal surface compared to other types of activated carbon.

Bei Verbrennungsanlagen, in denen große Mengen Verbrennungsabgase entstehen, beispielsweise in Kraftwerken, ist es vorteilhaft, dass das Adsorptionsmittel nach dem in Kontakt bringen mit einer ein Oxidationsmittel enthaltenden Lösung abgetrennt und rezirkuliert wird. Auf diese Weise lassen sich die Anschaffungskosten für das Adsorptionsmittel senken und die bei einer Verbrennung des Adsorptionsmittels entstehenden Umweltbelastungen werden vermieden.In incinerators where large quantities of combustion exhaust gases are generated, for example, in power plants, it is advantageous that the adsorbent is separated and recirculated after being contacted with a solution containing an oxidizer. In this way, the initial cost of the adsorbent can be reduced and the environmental pollution resulting from combustion of the adsorbent can be avoided.

Nachfolgend wird die Erfindung anhand eines bevorzugten Ausführungsbeispiels des erfindungsgemäßen Verfahrens in Verbindung mit der beiliegenden Zeichnung näher erläutert. Die Zeichnung zeigt ein Ablaufschema eines Ausführungsbeispiels des erfindungsgemäßen Verfahrens.The invention will be explained in more detail with reference to a preferred embodiment of the method according to the invention in conjunction with the accompanying drawings. The drawing shows a flow chart of an embodiment of the method according to the invention.

Das in dem Ablaufschema gezeigte Ausführungsbeispiel des erfindungsgemäßen Verfahrens betrifft eine Verbrennungsabgasreinigung für einen 500MW-Block eines Kraftwerks.The embodiment of the inventive method shown in the flowchart relates to a combustion exhaust gas purification for a 500 MW block of a power plant.

Von der Verbrennungseinrichtung (1) gelangen die Verbrennungsabgase zur Entstickungseinrichtung (2), mit welcher die Stickoxide aus den Verbrennungsabgasen entfernt werden. Die Entstickungseinrichtung kann gemäß einem dem Fachmann bekannten Verfahren, wie beispielsweise der selektiven nichtkatalytischen oder katalytischen Entstickung, betrieben werden.From the combustion device (1), the combustion exhaust gases reach the denitrification device (2), with which the nitrogen oxides are removed from the combustion exhaust gases. The denitrification device can be operated in accordance with a method known to those skilled in the art, such as selective non-catalytic or catalytic denitrification.

Die entstickten Abgase gelangen in eine Entstaubungsanlage (3), in welcher Flugstaub aus den Verbrennungsabgasen entfernt wird. Bei Kraftwerken wird zur Entstaubung der Verbrennungsabgase zumeist ein Elektrofilter verwendet.The denitrated exhaust gases pass into a dedusting system (3), in which flue dust is removed from the combustion exhaust gases becomes. In power plants, an electrostatic precipitator is usually used to dedust the combustion gases.

Nach welchem Verfahren genau die Entstickung und die Entstaubung vorgenommen werden, hat jedoch auf die vorliegende Erfindung keinen Einfluss - diese beiden Arbeitsschritte sind lediglich der Vollständigkeit halber dargestellt.However, according to which method exactly the denitrification and dedusting are carried out, the present invention has no influence - these two working steps are shown only for the sake of completeness.

Nach der Entstaubung der Verbrennungsabgase gelangen diese in die Entschwefelungsanlage bzw. den REA-Wäscher (4). Bei dem hier gezeigten Ausführungsbeispiel des erfindungsgemäßen Verfahrens wird das in den Verbrennungsabgasen vorhandene Schwefeldioxid mit einem Sprühadsorptionsverfahren entfernt, bei welchem eine basische Kalkhydratsuspension in die zu reinigenden Verbrennungsabgase eingesprüht wird. Das bei der Umsetzung mit Schwefeldioxid entstehende CaSO3 wird beispielsweise mit Luftsauerstoff zur CaSO4 aufoxidiert. Bei dieser Oxidation wird auch ggf. noch in den Verbrennungsabgasen vorhandenes Hg1+ zu Hg2+ oxidiert. Bei alternativen Ausführungsbeispielen können andere Entschwefelungsverfahren verwendet werden - beispielsweise die Entschwefelung mit Ammoniak.After the dedusting of the combustion exhaust gases they reach the desulphurisation plant or the REA scrubber (4). In the embodiment of the method according to the invention shown here, the sulfur dioxide present in the combustion exhaust gases is removed by a spray adsorption process in which a basic hydrated lime suspension is sprayed into the combustion exhaust gases to be purified. The resulting in the reaction with sulfur dioxide CaSO 3 is oxidized, for example, with atmospheric oxygen to CaSO 4 . During this oxidation Hg 1+ , which may still be present in the combustion exhaust gases, is also oxidized to Hg 2+ . In alternative embodiments, other desulfurization processes may be used - for example desulfurization with ammonia.

In den sogenannten Sumpf des REA-Wäschers (4) werden Aktivkohlepartikel als Adsorptionsmittel gegeben. Die Aktivkohlepartikel adsorbieren das von den Verbrennungsabgasen in die REA-Wäscherlösung übergegangene Hg2+. Bei alternativen Ausführungsbeispielen ist es beispielsweise denkbar, feine Aktivkohlepartikel stromauf des REA-Wäschers in die Verbrennungsgase einzublasen. In einem solchen Fall wird ein Teil des in den Verbrennungsabgasen vorliegenden Quecksilbers von den Aktivkohlepartikeln bereits aus den Verbrennungsabgasen selber adsorbiert. Das nicht adsorbierte Quecksilber geht in dem REA-Wäscher in Lösung und wird dort von den Aktivkohlepartikeln adsorbiert.In the so-called bottom of the REA scrubber (4) activated carbon particles are added as adsorbent. The activated carbon particles adsorb the Hg 2+ transferred from the combustion exhaust gases to the REA scrubber solution. For example, in alternative embodiments, it is conceivable to inject fine activated carbon particles into the combustion gases upstream of the REA scrubber. In such a case, part of the mercury present in the combustion exhaust gases is already adsorbed by the activated carbon particles from the combustion exhaust gases themselves. The unadsorbed mercury goes into solution in the REA scrubber where it is adsorbed by the activated carbon particles.

Bei einer Verbrennungsanlage mit 500MW entstehen pro Stunde etwa 1,5 Mio. m3 Verbrennungsabgase. Bei einem Quecksilbergehalt von < 0,50 mg pro Kilo Kohle müssen pro Stunde lediglich etwa 4 kg Aktivkohle zugeführt werden. In dem REA-Wäscher liegt die Konzentration der Aktivkohlepartikel bei einer solchen Zugabe bei ungefähr 100 mg/l.In an incinerator with 500MW, about 1.5 million m 3 of combustion gases are produced per hour. With a mercury content of <0.50 mg per kilo of coal, only about 4 kg of activated carbon need be added per hour. In the REA scrubber, the concentration of activated carbon particles at such an addition is about 100 mg / L.

Die in dem REA-Wäscher entstehende Suspension, die unter anderem Gips, weitere Feststoffe sowie Aktivkohlepartikel enthält, wird in einen Gips-Zyklon (5) geführt, welcher die in dem REA-Wäscher entstandene Suspension in zwei Phasen trennt, nämlich in das schwere kristalline CaSO4 sowie eine Suspension, die die leichten Aktivkohlepartikel sowie weitere amorphe und somit leichte Feststoffe, wie beispielsweise Staub und Metallhydroxide, enthält. Der Gipsweißgrad wird durch die Hinzufügung von Aktivkohle nur unwesentlich vermindert, und zwar von ungefähr 74% auf 72%.The resulting in the REA scrubber suspension containing, inter alia, gypsum, other solids and activated carbon particles is fed into a gypsum cyclone (5), which separates the resulting in the REA scrubber suspension into two phases, namely in the heavy crystalline CaSO 4 and a suspension containing the light activated carbon particles as well as other amorphous and thus light solids such as dust and metal hydroxides. The degree of gypsum whiteness is only marginally reduced by the addition of activated carbon, from about 74% to 72%.

Die den Gips-Zyklon (5) verlassende Suspension wird in einen Abwasser-Zyklon (6) geführt. In diesem Abwasser-Zyklon (6) wird ein Teil des Abwassers von der Suspension abgetrennt und man erhält eine Suspension mit einem höheren Feststoffanteil. Gegenüber der Suspension aus dem Gips-Zyklon (5) ist das Volumen dieser Suspension aus dem Abwasser-Zyklon (6) stark vermindert, so dass nachfolgende Verfahrensschritte anlagentechnisch weniger aufwendig gestaltet werden können.The gypsum cyclone (5) leaving suspension is fed into a wastewater cyclone (6). In this wastewater cyclone (6) a part of the waste water is separated from the suspension and gives a suspension with a higher solids content. Compared to the suspension from the gypsum cyclone (5), the volume of this suspension from the wastewater cyclone (6) is greatly reduced, so that subsequent process steps can be made less expensive plant technology.

Das den Abwasser-Zyklon (6) verlassende Abwasser weist eine Quecksilberkonzentration von nur noch ungefähr 10 µg/l auf. Das Abwasser wird zum Teil in das Verfahren rezirkuliert, oder es wird einer Abwasseranlage zugeführt. Aufgrund des geringen Quecksilbergehaltes kann der in der Abwasseranlage entstehende RAA-Schlamm verbrannt werden - eine Deponierung ist nicht mehr erforderlich.The wastewater cyclone (6) leaving wastewater has a mercury concentration of only about 10 micrograms / l. The wastewater is partially recirculated to the process, or it is fed to a wastewater treatment plant. Due to the low mercury content, the RAA sludge produced in the wastewater plant can be incinerated - landfilling is no longer required.

Das erfindungsgemäße Verfahren ist jedoch nicht auf die bei diesem Ausführungsbeispiel dargestellte Trennung der Aktivkohle sowie anderer Feststoffe von dem Abwasser bzw. den Verbrennungsgasen beschränkt. Neben der Verwendung eines Gips-Zyklons und eines Abwasser-Zyklons kann die Abtrennung auch mit anderen, dem Fachmann bekannten Trennmethoden erfolgen. Das obige Trennverfahren ist jedoch bevorzugt, da es eine Trennung in Gips, Abwasser sowie eine feststoffhaltige Suspension mit einfachen Mitteln ermöglicht.The inventive method is not limited to the illustrated in this embodiment separation of the activated carbon and other solids from the wastewater or the combustion gases. Apart from the use of a gypsum cyclone and a wastewater cyclone, the separation can also be carried out with other separation methods known to the person skilled in the art. However, the above separation method is preferred because it allows separation into gypsum, waste water and a solids-containing suspension with simple means.

Bei einem nachfolgenden Verfahrensschritt wird in die Suspension aus dem Abwasser-Zyklon (6), die die Aktivkohlepartikel und weitere Feststoffen enthält, eine wässrige Natriumhypochloritlösung mit einem pH-Wert von ca. 6,5 eingeleitet. Pro Liter Suspension werden 1 - 4 ml einer ca. 13%-igen Natriumhypochloritlösung eingeleitet. Um ein Absetzen der Feststoffe bereits zu diesem Zeitpunkt zu verhindern, wird die Lösung mit einer geeigneten Rühreinrichtung durchmischt. Bei alternativen Ausführungsbeispielen können selbstverständlich andere Oxidationsmittel in einem anderen pH-Bereich verwendet werden. Während der Behandlung mit dem Oxidationsmittel löst sich das Quecksilber wieder von der Aktivkohle und geht als Hg2+ in Lösung.In a subsequent process step, an aqueous sodium hypochlorite solution is introduced into the suspension from the wastewater cyclone (6), which contains the activated carbon particles and further solids initiated with a pH of about 6.5. Per liter of suspension, 1 - 4 ml of an approx. 13% sodium hypochlorite solution are introduced. To prevent settling of the solids already at this time, the solution is mixed with a suitable stirring device. Of course, alternative embodiments may use other oxidants in a different pH range. During treatment with the oxidizing agent, the mercury dissolves again from the activated carbon and goes into solution as Hg 2+ .

Nachdem das Quecksilber vollständig in Lösung gegangen ist, was von der jeweils verwendeten Aktivkohle sowie der Konzentration des Oxidationsmittels sowie der Temperatur abhängt, wird die Lösung mit einem Flockungshilfsmittel und/oder einem Flockungsmittel sowie, zur Erhöhung des pH-Wertes der Lösung, mit Ca(OH)2 versetzt. Die Lösung wird dabei auf einen pH-Wert von ungefähr 8,5 eingestellt. Die Erhöhung des pH-Wertes geschieht zum einen aufgrund von gesetzlichen Vorgaben, die besagen, dass Abwässer einer Abwasserreinigungsanlage einen in einem gewissen pH-Wertfenster liegenden pH-Wert aufweisen müssen, und zum anderen, um für eine Gips-Entsättigung der Lösung zu sorgen. Dies bedeutet, dass bei Zugabe des Ca(OH)2 weiteres Calciumsulfat aus der Lösung ausfällt. Ferner fallen bei Erhöhung des pH-Wertes weitere Metallhydroxide, wie beispielsweise Nickel- und Kupferhydroxid, aus der Lösung aus.After the mercury has completely dissolved, depending on the particular activated carbon used and the concentration of the oxidizing agent and the temperature, the solution is treated with a flocculant and / or a flocculant and with Ca (to increase the pH of the solution). OH) 2 offset. The solution is adjusted to a pH of about 8.5. The increase in the pH occurs on the one hand due to legal requirements, which state that wastewater from a wastewater treatment plant must have a lying in a certain pH window pH value, and on the other, to provide a gypsum desaturation of the solution. This means that upon addition of the Ca (OH) 2 additional calcium sulfate precipitates out of the solution. Furthermore, when the pH is increased, further metal hydroxides, such as, for example, nickel hydroxide and copper hydroxide, precipitate out of the solution.

Unter Flockungsmitteln versteht man Stoffe, die Teilchen in einer Suspension derart beeinflussen, dass diese zu Flocken (Mikroflocken) aggregieren und daher aus der Suspension entfernt werden können. Als Flockungsmittel wird im vorliegenden Ausführungsbeispiel vorzugsweise Eisen(III)chlorid, Eisen(III)sulfat oder eine Mischung dieser Salze verwendet. Welches dieser Salze eingesetzt wird, hängt von der momentanen Verfügbarkeit ab. Bei Zugabe dieser Salze entsteht ein voluminöser Fe(OH)3-Niederschlag, der sich mit anderen weniger voluminösen Feststoffen zusammenballt. Um die Absetzgeschwindigkeit der aggregierten Teilchen zu beschleunigen und eine Abtrennung dieser zu vereinfachen, kann ein sogenanntes Flokkungshilfsmittel zugesetzt werden, welches die Zusammenballung von Feststoffpartikeln zu größeren Einheiten (Makroflocken) bewirkt, die sich aufgrund ihrer größeren Masse schneller absetzen können und einfacher abgetrennt werden können. Als Flockungshilfsmittel werden im vorliegenden Ausführungsbeispiel bevorzugt anionische Polymere zugesetzt. Ob und im welchem Umfang ein Flockungsmittel bzw. ein Flockungshilfsmittel zugesetzt wird, hängt von der Zusammensetzung der Suspension und somit von der Verfahrensführung sowie der Zusammensetzung der Verbrennungsabgase ab.Flocculants are substances which influence particles in a suspension in such a way that they aggregate into flakes (microflakes) and can therefore be removed from the suspension. The flocculant used in the present embodiment is preferably iron (III) chloride, iron (III) sulfate or a mixture of these salts. Which of these salts is used depends on the current availability. Addition of these salts produces a voluminous Fe (OH) 3 precipitate which coalesces with other less bulky solids. In order to accelerate the settling speed of the aggregated particles and to facilitate separation thereof, a so-called flocculation aid may be used be added, which causes the aggregation of solid particles into larger units (macroflakes), which can settle faster due to their larger mass and can be separated easily. As flocculants, anionic polymers are preferably added in the present embodiment. Whether and to what extent a flocculant or a flocculant is added depends on the composition of the suspension and thus on the process control and the composition of the combustion exhaust gases.

Die nach der obigen Behandlung in der Suspension enthaltenen Feststoffe, die nun weitgehend quecksilberfrei sind, werden nachfolgend in einer Filterpresse von der quecksilberhaltigen Lösung getrennt. Bei dem hier beschriebenen Ausführungsbeispiel fallen pro Tag etwa 20 Tonnen Feststoffe an, bei denen der Quecksilbergehalt unter 10g/t liegt. Aufgrund dieses geringen Quecksilbergehalts können die Feststoffe verbrannt werden und es entstehen somit keine Kosten für eine Deponierung. Bei einem anderen Ausführungsbeispiel können die Feststoffe auch durch Sedimentation oder Flotation abgetrennt werden.The solids present in the suspension after the above treatment, which are now substantially free of mercury, are subsequently separated from the mercury-containing solution in a filter press. In the embodiment described here accumulate per day about 20 tons of solids at which the mercury content is below 10g / t. Due to this low mercury content, the solids can be incinerated and thus there are no costs for landfilling. In another embodiment, the solids may also be separated by sedimentation or flotation.

Zur Ausfällung des Quecksilbers wird die quecksilberhaltige Lösung wird mit einem Organosulfid, einem Flockungsmittel und einem Flockungshilfsmittel versetzt. Als Flockungsmittel wird vorzugsweise Eisen(III)chlorid eingesetzt, da dieses preisgünstig zu beziehen ist. Als Organosulfid wird vorzugsweise ein oxidationsbeständiges Organosulfid zugesetzt, da die Lösung ein hohes Oxidationspotential aufweisen kann. Um bereits zu diesem Zeitpunkt ein Absetzen des Organoquecksilbersulfids zu vermeiden, wird die Lösung in diesem Stadium mit einer geeigneten Rühreinrichtung durchmischt.To precipitate the mercury, the mercury-containing solution is treated with an organosulfide, a flocculant and a flocculant. As a flocculant iron (III) chloride is preferably used, since this is inexpensive to obtain. As the organosulfide, an oxidation-resistant organosulfide is preferably added because the solution may have a high oxidation potential. To avoid settling of the Organoquecksilbersulfids already at this time, the solution is mixed at this stage with a suitable stirring device.

Nachdem das Quecksilber als Organoquecksilbersulfid ausgefällt wurde, werden die Feststoffe über eine Membranfilterpresse abgetrennt und deponiert. Bei dem hier beschriebenen Ausführungsbeispiel fallen so pro Tag etwa 0,2 t Organoquecksilbersulfid-haltige Abfälle an.After the mercury has been precipitated as Organoquecksilbersulfid, the solids are separated and deposited via a membrane filter press. In the exemplary embodiment described here, about 0.2 t of organo-mercury sulfide-containing waste accumulates per day.

Claims (10)

Verfahren zum Entfernen von Quecksilber aus Verbrennungsabgasen, aufweisend die Schritte: a) in Kontakt bringen von in den Verbrennungsabgasen enthaltenem Quecksilber mit einem Adsorptionsmittel, wobei das Quecksilber von dem Adsorptionsmittel weitgehend adsorbiert wird, b) Trennen des Adsorptionsmittels von den Verbrennungsabgasen, c) in Kontakt bringen des Adsorptionsmittels mit einer ein Oxidationsmittel enthaltenden wässrigen Lösung, wodurch das adsorbierte Quecksilber als Hg2+ in Lösung geht, d) Trennen der Hg2+-haltigen Lösung von dem Adsorptionsmittel, und e) Entfernen des Hg2+ aus der Lösung. Method for removing mercury from combustion exhaust gases, comprising the steps of: a) contacting mercury contained in the combustion exhaust gases with an adsorbent, the mercury being largely adsorbed by the adsorbent, b) separating the adsorbent from the combustion exhaust gases, c) contacting the adsorbent with an aqueous solution containing an oxidizing agent, whereby the adsorbed mercury goes into solution as Hg 2+ , d) separating the Hg 2+ -containing solution from the adsorbent, and e) removing the Hg 2+ from the solution. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass das Hg2+ aus der Lösung entfernt wird, indem die Hg2+-haltige Lösung mit einem Fällungsmittel versetzt wird, das mit Hg2+ einen schwerlöslichen Niederschlag bildet, und dieser von der Lösung abgetrennt wird.A method according to claim 1, characterized in that the Hg 2+ is removed from the solution by the Hg 2+ -containing solution is treated with a precipitant which forms a sparingly soluble precipitate with Hg 2+ , and this is separated from the solution , Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass als Fällungsmittel ein Organosulfid verwendet wird.A method according to claim 2, characterized in that an organosulfide is used as precipitant. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass das Hg2+ aus der Lösung entfernt wird, indem die Lösung mit einem Ionenaustauscher in Kontakt gebracht wird.A method according to claim 1, characterized in that the Hg 2+ is removed from the solution by bringing the solution into contact with an ion exchanger. Verfahren einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass in den Verbrennungsabgasen enthaltenes Hg0 vor dem in Kontakt bringen von in den Verbrennungsabgasen enthaltenem Quecksilber mit dem Adsorptionsmittel oxidiert wird.Method according to one of claims 1 to 4, characterized in that Hg 0 contained in the combustion exhaust gases is oxidized with the adsorbent prior to contacting mercury contained in the combustion exhaust gases. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass das Adsorptionsmittel vor oder in einem REA-Wäscher den Verbrennungsabgasen zugeführt wird.Method according to one of claims 1 to 5, characterized in that the adsorbent is supplied to the combustion exhaust gases before or in a REA scrubber. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass in dem REA-Wäscher entstehende Feststoffe durch Fliehkraftabscheidung von dem Adsorptionsmittel getrennt werden.A method according to claim 6, characterized in that in the REA scrubber resulting solids are separated by centrifugal separation of the adsorbent. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass als Oxidationsmittel vorzugsweise Hypochlorit, Chlordioxid oder Chlorgas verwendet wird.Method according to one of claims 1 to 7, characterized in that is preferably used as the oxidizing agent hypochlorite, chlorine dioxide or chlorine gas. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, dass als Adsorptionsmittel Aktivkohle verwendet wird.Method according to one of claims 1 to 8, characterized in that activated carbon is used as the adsorbent. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, dass das Adsorptionsmittel nach dem in Kontakt bringen mit einer ein Oxidationsmittel enthaltenden Lösung abgetrennt und rezirkuliert wird.Method according to one of claims 1 to 9, characterized in that the adsorbent is separated and recirculated after contacting with a solution containing an oxidizing agent.
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SI200730566T SI2033702T1 (en) 2007-09-04 2007-09-04 Method for removing mercury from exhaust combustion gases
ES07115662T ES2359091T3 (en) 2007-09-04 2007-09-04 PROCEDURE FOR THE ELIMINATION OF MERCURY FROM COMBUSTION OUTPUT GASES.
PT07115662T PT2033702E (en) 2007-09-04 2007-09-04 Method for removing mercury from exhaust combustion gases
PL07115662T PL2033702T3 (en) 2007-09-04 2007-09-04 Method for removing mercury from exhaust combustion gases
AT07115662T ATE495812T1 (en) 2007-09-04 2007-09-04 METHOD FOR REMOVING MERCURY FROM COMBUSTION FUSES
DE502007006314T DE502007006314D1 (en) 2007-09-04 2007-09-04 Method for removing mercury from combustion exhaust gases
EP07115662A EP2033702B1 (en) 2007-09-04 2007-09-04 Method for removing mercury from exhaust combustion gases
DK07115662.4T DK2033702T3 (en) 2007-09-04 2007-09-04 Method of removing mercury from combustion gases
CA2616540A CA2616540C (en) 2007-09-04 2007-12-21 Method of removing mercury from combustion exhaust gases
US12/082,761 US7727307B2 (en) 2007-09-04 2008-04-14 Method for removing mercury from flue gas after combustion
TW097130913A TWI355289B (en) 2007-09-04 2008-08-14 Method of removing mercury from flue gas after com
ZA200807352A ZA200807352B (en) 2007-09-04 2008-08-26 Method of removing mercury from flue gas after combustion
AU2008207555A AU2008207555B2 (en) 2007-09-04 2008-08-27 Method of removing mercury from flue gas after combustion
KR1020080086802A KR101124058B1 (en) 2007-09-04 2008-09-03 Method of removing mercury from flue gas after combustion
JP2008225927A JP2009061450A (en) 2007-09-04 2008-09-03 Method for removing mercury from flue gas after combustion
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101869825A (en) * 2010-05-06 2010-10-27 同济大学 Preparation method of activated sludge mercury ion adsorbent
WO2013117341A1 (en) 2012-02-10 2013-08-15 Andritz Energy & Environment Gmbh Method for reducing the content of fine material in fgd gypsum
DE102014007746A1 (en) 2014-05-30 2015-12-03 Rwe Power Aktiengesellschaft A process for removing mercury from the scrubbing suspension of a wet scrubber and adsorbent for use in a wet scrubber
AT516734A4 (en) * 2015-04-15 2016-08-15 Andritz Ag Maschf Method for removing mercury from scrubber suspensions
CN114173905A (en) * 2019-05-13 2022-03-11 W.L.戈尔及同仁股份有限公司 Reduction of mercury vapor emissions

Families Citing this family (67)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007020855A1 (en) 2007-05-02 2008-11-06 Evonik Energy Services Gmbh Process for purifying flue gases from incineration plants
US8632742B2 (en) 2007-12-07 2014-01-21 Nalco Company Methods of controlling mercury emission
JP5231957B2 (en) * 2008-11-27 2013-07-10 バブコック日立株式会社 Wet desulfurization equipment
US8496894B2 (en) 2010-02-04 2013-07-30 ADA-ES, Inc. Method and system for controlling mercury emissions from coal-fired thermal processes
US8951487B2 (en) 2010-10-25 2015-02-10 ADA-ES, Inc. Hot-side method and system
US11298657B2 (en) 2010-10-25 2022-04-12 ADA-ES, Inc. Hot-side method and system
US9200225B2 (en) 2010-08-03 2015-12-01 Suncoke Technology And Development Llc. Method and apparatus for compacting coal for a coal coking process
US8845986B2 (en) 2011-05-13 2014-09-30 ADA-ES, Inc. Process to reduce emissions of nitrogen oxides and mercury from coal-fired boilers
US20130075316A1 (en) * 2011-09-25 2013-03-28 National Chi Nan University Method of treating water pollutant
US8480983B1 (en) * 2012-03-15 2013-07-09 Alstom Technology Ltd Mercury capture system and method for a wet flue gas desulfurization system
EP2827970B1 (en) 2012-03-22 2017-11-01 Saudi Arabian Oil Company Method for removing mercury from a liquid stream
US8883099B2 (en) 2012-04-11 2014-11-11 ADA-ES, Inc. Control of wet scrubber oxidation inhibitor and byproduct recovery
EP2879777B1 (en) 2012-07-31 2019-05-29 SunCoke Technology and Development LLC Methods for handling coal processing emissions and associated systems and devices
DE102012214065A1 (en) 2012-08-08 2014-02-13 EnBW Energie Baden-Württemberg AG Method of removing mercury from flue gas in a wet scrubber
US9957454B2 (en) 2012-08-10 2018-05-01 ADA-ES, Inc. Method and additive for controlling nitrogen oxide emissions
US9243186B2 (en) 2012-08-17 2016-01-26 Suncoke Technology And Development Llc. Coke plant including exhaust gas sharing
US9359554B2 (en) 2012-08-17 2016-06-07 Suncoke Technology And Development Llc Automatic draft control system for coke plants
US9249357B2 (en) 2012-08-17 2016-02-02 Suncoke Technology And Development Llc. Method and apparatus for volatile matter sharing in stamp-charged coke ovens
WO2014031623A1 (en) 2012-08-20 2014-02-27 Ecolab Usa Inc. Mercury sorbents
US9169439B2 (en) 2012-08-29 2015-10-27 Suncoke Technology And Development Llc Method and apparatus for testing coal coking properties
WO2014046701A1 (en) 2012-09-21 2014-03-27 Suncoke Technology And Development Llc. Reduced output rate coke oven operation with gas sharing providing extended process cycle
WO2014066175A1 (en) 2012-10-22 2014-05-01 Nalco Company Methods of controlling mercury emission
WO2014082076A1 (en) 2012-11-26 2014-05-30 Ecolab Usa Inc. Control of mercury emissions
US10883051B2 (en) 2012-12-28 2021-01-05 Suncoke Technology And Development Llc Methods and systems for improved coke quenching
BR112015015667A2 (en) 2012-12-28 2017-07-11 Suncoke Tech & Development Llc systems and methods for mercury removal from emissions
US10047295B2 (en) 2012-12-28 2018-08-14 Suncoke Technology And Development Llc Non-perpendicular connections between coke oven uptakes and a hot common tunnel, and associated systems and methods
WO2014105063A1 (en) 2012-12-28 2014-07-03 Suncoke Technology And Development Llc. Systems and methods for maintaining a hot car in a coke plant
US9238778B2 (en) 2012-12-28 2016-01-19 Suncoke Technology And Development Llc. Systems and methods for improving quenched coke recovery
US9476547B2 (en) 2012-12-28 2016-10-25 Suncoke Technology And Development Llc Exhaust flow modifier, duct intersection incorporating the same, and methods therefor
US9273249B2 (en) 2012-12-28 2016-03-01 Suncoke Technology And Development Llc. Systems and methods for controlling air distribution in a coke oven
CA2896478C (en) 2012-12-28 2016-06-07 Suncoke Technology And Development Llc. Vent stack lids and associated systems and methods
US20160158701A1 (en) * 2013-01-14 2016-06-09 Babcock & Wilcox Power Generation Group, Inc. Controlling aqcs parameters in a combustion process
US9193915B2 (en) 2013-03-14 2015-11-24 Suncoke Technology And Development Llc. Horizontal heat recovery coke ovens having monolith crowns
US9273250B2 (en) 2013-03-15 2016-03-01 Suncoke Technology And Development Llc. Methods and systems for improved quench tower design
EP2971961A4 (en) 2013-03-15 2016-11-23 Ecolab Usa Inc Method of oxidizing mercury in flue gas
AR095224A1 (en) * 2013-03-15 2015-09-30 Albemarle Corp INJECTION OF SORBENTS IN WET TREATMENTS OF DRUG FEEDING FOR THE CONTROL OF EMISSION OF MERCURY
US9889451B2 (en) 2013-08-16 2018-02-13 ADA-ES, Inc. Method to reduce mercury, acid gas, and particulate emissions
WO2015103414A1 (en) 2013-12-31 2015-07-09 Suncoke Technology And Development Llc Methods for decarbonizing coking ovens, and associated systems and devices
US10307706B2 (en) 2014-04-25 2019-06-04 Ada Carbon Solutions, Llc Sorbent compositions for use in a wet scrubber unit
US10526541B2 (en) 2014-06-30 2020-01-07 Suncoke Technology And Development Llc Horizontal heat recovery coke ovens having monolith crowns
US9708542B2 (en) 2014-08-28 2017-07-18 Suncoke Technology And Development Llc Method and system for optimizing coke plant operation and output
EP3194531A4 (en) 2014-09-15 2018-06-20 Suncoke Technology and Development LLC Coke ovens having monolith component construction
US10968395B2 (en) 2014-12-31 2021-04-06 Suncoke Technology And Development Llc Multi-modal beds of coking material
US11060032B2 (en) 2015-01-02 2021-07-13 Suncoke Technology And Development Llc Integrated coke plant automation and optimization using advanced control and optimization techniques
WO2016109854A1 (en) 2015-01-02 2016-07-07 Suncoke Technology And Development Llc Integrated coke plant automation and optimization using advanced control and optimization techniques
US9797598B1 (en) 2015-03-25 2017-10-24 Great River Energy Method for controlling gaseous mercury emission between two or more coal-fired combustion units
PL3281686T3 (en) 2015-04-09 2020-07-13 Mitsubishi Hitachi Power Systems, Ltd. Method and device for wet flue-gas desulfurization
DE102015218462A1 (en) 2015-09-25 2017-03-30 EnBW Energie Baden-Württemberg AG Apparatus supplementation of wet scrubbers in coal-fired power stations for better and safer separation of mercury and its compounds
KR102253567B1 (en) 2015-12-28 2021-05-17 선코크 테크놀러지 앤드 디벨로프먼트 엘엘씨 Method and system for dynamically filling a coke oven
MX2018000954A (en) 2016-06-03 2018-06-07 Suncoke Tech & Development Llc Methods and systems for automatically generating a remedial action in an industrial facility.
JP7154231B2 (en) 2017-05-23 2022-10-17 サンコーク テクノロジー アンド ディベロップメント リミテッド ライアビリティ カンパニー Systems and methods for refurbishing coke ovens
US11319233B2 (en) 2018-08-17 2022-05-03 Steve Feeney Consulting, Llc Control of aqueous arsenic, selenium, mercury or other metals from flue gas
CA3124590C (en) 2018-12-28 2023-08-22 Suncoke Technology And Development Llc Systems and methods for treating a surface of a coke plant
US11071935B2 (en) 2018-12-28 2021-07-27 Suncoke Technology And Development Llc Particulate detection for industrial facilities, and associated systems and methods
US11760937B2 (en) 2018-12-28 2023-09-19 Suncoke Technology And Development Llc Oven uptakes
BR112021012511B1 (en) 2018-12-28 2023-05-02 Suncoke Technology And Development Llc SPRING LOADED HEAT RECOVERY FURNACE SYSTEM AND METHOD
CA3125332C (en) 2018-12-28 2022-04-26 Suncoke Technology And Development Llc Decarbonization of coke ovens, and associated systems and methods
WO2020140092A1 (en) 2018-12-28 2020-07-02 Suncoke Technology And Development Llc Heat recovery oven foundation
US11395989B2 (en) 2018-12-31 2022-07-26 Suncoke Technology And Development Llc Methods and systems for providing corrosion resistant surfaces in contaminant treatment systems
BR122023020289A2 (en) 2018-12-31 2024-01-23 SunCoke Technology and Development LLC COKE PLANT AND METHOD OF MODIFYING A HEAT RECOVERY VALUE GENERATOR (HRSG)
CN113578030B (en) * 2020-04-30 2024-01-26 黄华丽 Absorbent slurry for removing mercury in flue gas and preparation and removal methods thereof
CA3177017C (en) 2020-05-03 2024-04-16 John Francis Quanci High-quality coke products
CN111773921B (en) * 2020-07-08 2022-03-08 山东康源环保科技有限公司 Coking VOCS tail gas treatment device
CN112058224A (en) * 2020-08-28 2020-12-11 贵州省材料产业技术研究院 Preparation method of composite biochar modified material for removing mercury in sewage
KR20230164076A (en) 2021-11-04 2023-12-01 선코크 테크놀러지 앤드 디벨로프먼트 엘엘씨 Foundry coke products and related systems, devices and methods
US11946108B2 (en) 2021-11-04 2024-04-02 Suncoke Technology And Development Llc Foundry coke products and associated processing methods via cupolas
WO2024098010A1 (en) 2022-11-04 2024-05-10 Suncoke Technology And Development Llc Coal blends, foundry coke products, and associated systems, devices, and methods

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5695726A (en) * 1993-06-10 1997-12-09 Beco Engineering Company Removal of mercury and cadmium and their compounds from incinerator flue gases
JP2006035042A (en) * 2004-07-23 2006-02-09 Mitsubishi Heavy Ind Ltd Regeneration method of gas purifying apparatus, and gas purifying method using the same
US7033419B1 (en) * 2003-09-16 2006-04-25 The United States Of America As Represented By The United States Department Of Energy Method for high temperature mercury capture from gas streams
US20070140940A1 (en) * 2005-12-15 2007-06-21 The United States Of America, As Represented By The Administrator Of The U.S. Environ. Agcy. Compositions and methods for removing mercury from mercury-containing fluids
US20070167309A1 (en) * 2003-04-23 2007-07-19 Olson Edwin S Process for regenerating a spent sorbent

Family Cites Families (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5830345A (en) 1981-08-19 1983-02-22 Mitsubishi Heavy Ind Ltd Catalyst activation method
EP0161206A3 (en) * 1984-04-03 1987-11-04 Mitsubishi Jukogyo Kabushiki Kaisha Method for regenerating a denitration catalyst
EP0159959B1 (en) * 1984-04-05 1992-01-15 Mitsubishi Jukogyo Kabushiki Kaisha Method for recovering denitrating catalyst for ammonia catalytic reduction
DE3742063A1 (en) * 1987-12-11 1989-06-22 Varta Batterie METHOD FOR DETOXIFYING SEWAGE CONTAINING ELEMENTAL MERCURY
JP2594301B2 (en) * 1988-01-19 1997-03-26 バブコツク日立株式会社 Coal-fired boiler with denitration equipment
DE3810137A1 (en) 1988-03-25 1989-10-05 Iss Gradewald Ind Schiffs Serv METHOD FOR CLEANING HOLLOW BODIES AND DEVICE FOR CARRYING OUT THE METHOD
DE3816600A1 (en) 1988-05-14 1989-11-23 Huels Chemische Werke Ag Process for the regeneration of arsenic-contaminated catalysts and sorbents
DE3824464A1 (en) 1988-07-19 1990-01-25 Basf Ag METHOD FOR REGENERATING CATALYSTS
DE4110337A1 (en) * 1991-03-28 1992-10-01 Siemens Ag METHOD AND DEVICE FOR REGENERATING CONSUMED DENO (DOWN ARROW) X (DOWN ARROW) CATALYSTS
DE4300933C1 (en) 1993-01-15 1994-05-19 Huels Chemische Werke Ag Titania denitrification catalyst regeneration to remove arsenic - by contact with gas contg. hydrogen, then oxidising gas in simple, effective non-destructive process
WO1995020434A1 (en) * 1994-01-27 1995-08-03 Engelhard Corporation Process for recovering catalyst supports
AT400114B (en) 1994-04-15 1995-10-25 Integral Umwelt Und Anlagentec PLANT AND METHOD FOR CATALYTICALLY REDUCING STICKOXIDES CONTAINED IN THE SMOKE GASES OF A FIRE WITH LIQUID FUELS WITH AMMONIA, PLANT FOR BURNING LIQUID FOSSIL FUELS AND METHOD FOR REGULATING A CATALYST
ES2097699B1 (en) * 1994-10-26 1997-12-16 Asturiana De Zinc Sa CONTINUOUS PROCEDURE FOR THE SIMULTANEOUS COLLECTION AND PRECIPITATION OF MERCURY IN GASES CONTAINING IT.
DE4441090A1 (en) * 1994-11-18 1996-05-23 Steag Ag Method and device for cleaning combustion exhaust gases
DE19533912C2 (en) 1995-09-13 1998-09-24 Gutehoffnungshuette Man Refractory lining for a synthesis gas plant
DE19542065C2 (en) * 1995-11-13 1997-10-23 Steag Ag Method and device for cleaning combustion gases from combustion plants
JP3297305B2 (en) * 1996-06-13 2002-07-02 三菱重工業株式会社 Method for removing clogged dust from honeycomb catalyst
JP3389005B2 (en) * 1996-06-25 2003-03-24 三菱重工業株式会社 Nitrogen oxide removal catalyst
DE19628212B4 (en) 1996-07-12 2008-06-05 Enbw Energy Solutions Gmbh Process for purifying and / or regenerating completely or partially deactivated catalysts for denitrification of flue gases
TW436332B (en) 1996-08-19 2001-05-28 Siemens Ag Process and equipment for cleaning of contaminated object
DE19652563A1 (en) * 1996-12-17 1998-06-18 Heidenhain Gmbh Dr Johannes Photoelectric position measuring device
JP3377715B2 (en) * 1997-02-27 2003-02-17 三菱重工業株式会社 Regeneration method of denitration catalyst
DE19723796C2 (en) * 1997-06-06 2003-07-17 Saar En Gmbh Process for reactivating honeycomb-shaped catalyst elements for the denitrification of flue gases
EP0936166A1 (en) 1998-02-10 1999-08-18 E.I. Du Pont De Nemours And Company High speed cutting assembly
DE19829916B4 (en) * 1998-07-06 2005-03-24 Envica Gmbh Process for the regeneration of catalysts and regenerated catalysts
DE19832057C1 (en) * 1998-07-16 2000-03-16 Siemens Ag Process for the regeneration of a deactivated catalyst
US6395665B2 (en) * 1998-07-24 2002-05-28 Mitsubishi Heavy Industries, Ltd. Methods for the regeneration of a denitration catalyst
DE59900514D1 (en) * 1998-08-26 2002-01-17 Integral Umwelt Und Anlagentec METHOD FOR REGENERATING USED DeNOx or Dedioxin CATALYSTS
US6455456B1 (en) 1999-11-29 2002-09-24 Hera, Llc Method for the in-situ cleaning of the catalytically active surfaces of SCR substrate
US6482762B1 (en) * 2000-08-14 2002-11-19 Atlantic Richfield Company NOx conversion catalyst rejuvenation process
WO2003014273A1 (en) * 2001-08-03 2003-02-20 Peter Morton A process for reducing the passive layer from the surface of a metal
DE10218380A1 (en) 2002-04-24 2003-11-20 Attila Kun Independent wheel suspension for vehicles, trailers or agricultural equipment
US6953494B2 (en) * 2002-05-06 2005-10-11 Nelson Jr Sidney G Sorbents and methods for the removal of mercury from combustion gases
DE10222915B4 (en) 2002-05-24 2013-03-28 Steag Power Saar Gmbh Process for the re-activation of honeycombed catalyst elements for the denitrification of flue gases
DE10233173B4 (en) * 2002-07-22 2006-03-23 Bayer Industry Services Gmbh & Co. Ohg Method for separating mercury from flue gases
DE10241004A1 (en) * 2002-09-05 2004-03-11 Envica Gmbh Process for the regeneration of iron-loaded Denox catalysts
DE10242081A1 (en) * 2002-09-11 2004-03-25 Envica Gmbh Regenerating phosphorus-contaminated denox catalysts by treatment with an aqueous alkaline solution, followed by neutralization with an acid
ATA2682003A (en) * 2003-02-21 2004-06-15 Envirgy Environment Energy Eng METHOD FOR REMOVING IMPURITIES AND / OR PLUGGINGS FROM A BUNCH OF CHANNELS
US6913026B2 (en) 2003-02-25 2005-07-05 Enerfab, Inc. Methods for cleaning catalytic converters
US6929701B1 (en) * 2003-06-03 2005-08-16 Scr-Tech Llc Process for decoating a washcoat catalyst substrate
DE10325779A1 (en) 2003-06-05 2005-01-05 Envica Gmbh Unblocking power station catalytic converter, comprises ultrasonic or electromagnetic loosening action and high pressure liquid scouring
KR100668936B1 (en) * 2004-10-29 2007-01-12 한국전력공사 Method of regenerating Honeycomb type SCR catalyst by air lift loop reactor
EP2258479A1 (en) * 2005-12-16 2010-12-08 Evonik Energy Services GmbH Process for the treatment of catalyst for the purification of flue gas
KR100760236B1 (en) * 2006-02-28 2007-10-04 한국과학기술연구원 Mercury control process from flue gas by halogenated compounds-impregnated activated carbon
US8375872B2 (en) * 2007-02-23 2013-02-19 Intertek APTECH Process for reduction of sulfur compounds and nitrogen compounds in the exhaust gases of combustion devices

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5695726A (en) * 1993-06-10 1997-12-09 Beco Engineering Company Removal of mercury and cadmium and their compounds from incinerator flue gases
US20070167309A1 (en) * 2003-04-23 2007-07-19 Olson Edwin S Process for regenerating a spent sorbent
US7033419B1 (en) * 2003-09-16 2006-04-25 The United States Of America As Represented By The United States Department Of Energy Method for high temperature mercury capture from gas streams
JP2006035042A (en) * 2004-07-23 2006-02-09 Mitsubishi Heavy Ind Ltd Regeneration method of gas purifying apparatus, and gas purifying method using the same
US20070140940A1 (en) * 2005-12-15 2007-06-21 The United States Of America, As Represented By The Administrator Of The U.S. Environ. Agcy. Compositions and methods for removing mercury from mercury-containing fluids

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101869825A (en) * 2010-05-06 2010-10-27 同济大学 Preparation method of activated sludge mercury ion adsorbent
CN101869825B (en) * 2010-05-06 2012-05-23 同济大学 Preparation method of activated sludge mercury ion adsorbent
WO2013117341A1 (en) 2012-02-10 2013-08-15 Andritz Energy & Environment Gmbh Method for reducing the content of fine material in fgd gypsum
US9139449B2 (en) 2012-02-10 2015-09-22 Andritz Ag Method for reducing the content of fine material in FGD gypsum
DE102014007746A1 (en) 2014-05-30 2015-12-03 Rwe Power Aktiengesellschaft A process for removing mercury from the scrubbing suspension of a wet scrubber and adsorbent for use in a wet scrubber
AT516734A4 (en) * 2015-04-15 2016-08-15 Andritz Ag Maschf Method for removing mercury from scrubber suspensions
AT516734B1 (en) * 2015-04-15 2016-08-15 Andritz Ag Maschf Method for removing mercury from scrubber suspensions
EP3081533A1 (en) * 2015-04-15 2016-10-19 Andritz AG Method for separation of mercury from washer suspensions
CN114173905A (en) * 2019-05-13 2022-03-11 W.L.戈尔及同仁股份有限公司 Reduction of mercury vapor emissions

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AU2008207555B2 (en) 2011-01-20
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JP2014155927A (en) 2014-08-28

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